CN109564771A - For operating the method and system of High pressure ethylene polymerization unit - Google Patents
For operating the method and system of High pressure ethylene polymerization unit Download PDFInfo
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- CN109564771A CN109564771A CN201780048102.2A CN201780048102A CN109564771A CN 109564771 A CN109564771 A CN 109564771A CN 201780048102 A CN201780048102 A CN 201780048102A CN 109564771 A CN109564771 A CN 109564771A
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- 238000000034 method Methods 0.000 title claims abstract description 79
- 238000006116 polymerization reaction Methods 0.000 title claims abstract description 20
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 239000005977 Ethylene Substances 0.000 title claims abstract description 17
- 238000005457 optimization Methods 0.000 claims abstract description 45
- 230000008569 process Effects 0.000 claims abstract description 33
- 239000003795 chemical substances by application Substances 0.000 claims description 39
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 238000004519 manufacturing process Methods 0.000 claims description 15
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 claims description 10
- 230000004907 flux Effects 0.000 claims description 6
- 239000003999 initiator Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 claims description 4
- 229920002554 vinyl polymer Polymers 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000004698 Polyethylene Substances 0.000 claims description 2
- 230000004913 activation Effects 0.000 claims description 2
- -1 polyethylene Polymers 0.000 claims description 2
- 229920000573 polyethylene Polymers 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims description 2
- 238000010791 quenching Methods 0.000 claims description 2
- 230000000171 quenching effect Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 238000012360 testing method Methods 0.000 claims description 2
- 229920000098 polyolefin Polymers 0.000 claims 4
- 229920001577 copolymer Polymers 0.000 claims 2
- 238000002360 preparation method Methods 0.000 claims 2
- 238000007689 inspection Methods 0.000 claims 1
- 238000004458 analytical method Methods 0.000 abstract description 5
- 230000008859 change Effects 0.000 description 10
- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical compound CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 description 6
- 230000006399 behavior Effects 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000012544 monitoring process Methods 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 230000004069 differentiation Effects 0.000 description 3
- 230000006870 function Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 210000004556 brain Anatomy 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000013473 artificial intelligence Methods 0.000 description 1
- 238000004422 calculation algorithm Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 230000000739 chaotic effect Effects 0.000 description 1
- 238000013480 data collection Methods 0.000 description 1
- 238000013135 deep learning Methods 0.000 description 1
- 238000009795 derivation Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
Classifications
-
- G—PHYSICS
- G16—INFORMATION AND COMMUNICATION TECHNOLOGY [ICT] SPECIALLY ADAPTED FOR SPECIFIC APPLICATION FIELDS
- G16C—COMPUTATIONAL CHEMISTRY; CHEMOINFORMATICS; COMPUTATIONAL MATERIALS SCIENCE
- G16C20/00—Chemoinformatics, i.e. ICT specially adapted for the handling of physicochemical or structural data of chemical particles, elements, compounds or mixtures
- G16C20/10—Analysis or design of chemical reactions, syntheses or processes
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F110/02—Ethene
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F210/02—Ethene
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F218/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an acyloxy radical of a saturated carboxylic acid, of carbonic acid or of a haloformic acid
- C08F218/02—Esters of monocarboxylic acids
- C08F218/04—Vinyl esters
- C08F218/08—Vinyl acetate
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B13/00—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion
- G05B13/02—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion electric
- G05B13/04—Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion electric involving the use of models or simulators
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B19/00—Programme-control systems
- G05B19/02—Programme-control systems electric
- G05B19/418—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS] or computer integrated manufacturing [CIM]
- G05B19/41875—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS] or computer integrated manufacturing [CIM] characterised by quality surveillance of production
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B19/00—Programme-control systems
- G05B19/02—Programme-control systems electric
- G05B19/418—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS] or computer integrated manufacturing [CIM]
- G05B19/41885—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS] or computer integrated manufacturing [CIM] characterised by modeling, simulation of the manufacturing system
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- G—PHYSICS
- G16—INFORMATION AND COMMUNICATION TECHNOLOGY [ICT] SPECIALLY ADAPTED FOR SPECIFIC APPLICATION FIELDS
- G16C—COMPUTATIONAL CHEMISTRY; CHEMOINFORMATICS; COMPUTATIONAL MATERIALS SCIENCE
- G16C20/00—Chemoinformatics, i.e. ICT specially adapted for the handling of physicochemical or structural data of chemical particles, elements, compounds or mixtures
- G16C20/30—Prediction of properties of chemical compounds, compositions or mixtures
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2400/00—Characteristics for processes of polymerization
- C08F2400/04—High pressure, i.e. P > 50 MPa, 500 bars or 7250 psi
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
- C08F2500/01—High molecular weight, e.g. >800,000 Da.
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- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B15/00—Systems controlled by a computer
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- G05—CONTROLLING; REGULATING
- G05B—CONTROL OR REGULATING SYSTEMS IN GENERAL; FUNCTIONAL ELEMENTS OF SUCH SYSTEMS; MONITORING OR TESTING ARRANGEMENTS FOR SUCH SYSTEMS OR ELEMENTS
- G05B19/00—Programme-control systems
- G05B19/02—Programme-control systems electric
- G05B19/418—Total factory control, i.e. centrally controlling a plurality of machines, e.g. direct or distributed numerical control [DNC], flexible manufacturing systems [FMS], integrated manufacturing systems [IMS] or computer integrated manufacturing [CIM]
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Abstract
This application discloses the high pressure polymerization process and system of a kind of operation order logic using optimization, the operation order logic of the optimization is at least partly established from the analysis of the database comprising prior operation data.The operation order logic of this optimization and the current process and system data of collection are used to automate the operation of High pressure ethylene polymerization process and unit.
Description
Cross reference to related applications
This application claims the equity of the priority of the USSN 62/356,846 submitted for 30th for 06 month in 2016, are led to
It crosses to refer to and is fully incorporated the present invention.
Invention field
The present invention relates to a kind of for operating the method and system of High pressure ethylene polymerization unit.Particularly, the present invention relates to
A kind of method and system of the operation order logic using optimization, the operation order logic of the optimization automate High pressure ethylene polymerization
The operation of unit.
Background of invention
High-pressure reactor, such as tubular reactor and autoclave, for the polymerization of ethylene under high pressure, such as higher than
1000 bars (100MPa) and 3000 bars of highest (300MPa) or higher pressure.In these methods, ethylene source of supply is come from
Fresh ethylene reactor pressure and later in the reactor and such as is successively compressed to by main compressor and the second compressor
Initiator existing for fruit and the mixing of any comonomer, and being polymerize to obtain includes principal polymeric and unreacted monomer
Mixture.This mixture leaves reactor by valve, which is commonly referred to as high pressure discharge gate, and enters later
Separation system, in the suction inlet that wherein unreacted monomer separated and be recycled back into secondary compressor with polymer,
It merges with the fresh ethylene from main compressor there.
ExxonMobil on 06 23rd, 2015 announce come into operation Honeywell procedural operation scheme at it
Oil plant and chemical plant installations improvement profit, reduction workload (http://www.controlglobal.com/articles/ 2015/hug-8/)。
Currently, high pressure polymerisation process and the operation sequence of reactor are carried out by operator, it is limited to by manual operation
Unstability lead to the disadvantage that, including operator empirical loss caused by being had enough to meet the need due to personnel, due to not being inconsistent with standardization program
The substandard product of conjunction, and optimal reactor control is inferior to caused by latest data as missing usage history data
System.Therefore, this field, which still needs, can provide vinyl polymerization unit improved control and the chaotic solution occurred of reduction operation
Certainly scheme.It is found by the applicant that this purpose can replace traditionally being carried out by operator by using the operation order logic of optimization
Complex operations process realize, may include the collecting and distributing control of the operative knowledge of multiple common copy operation persons and engineer
System (DCS) program.Particularly, the knowledge of experienced operator crawl (is solved) to exist including failure in an abnormal situation
Allow in program and operator interface therewith operation sequence automate and, successively, the behavior in response to real time reaction device condition can
To carry out automatically.The operation order logic of this optimization can transmit the stability of desired continuity and human expert's technology,
Simultaneously again reduce operation during human error a possibility that, so as to cause vinyl polymerization unit effective and steady running and subtract
The interruption from unexpected confusion is lacked.
Summary of the invention
Present invention offer can be a kind of for operating the method and system of High pressure ethylene polymerization unit.
The described method includes: (I) collects the data from prior operation；(II) number of the prior operation including collecting is established
According to database；(III) database is analyzed；(IV) the operation order logic of optimization is established；(V) the current of current operation is collected
Data；And (VI) carries out current operation according to the operation order logic and current data of optimization.
The method may include at least execute one or more of step (IV), (V) and (VI) following process: starting
Reactor in vinyl polymerization unit；Operation is converted to from the optimal conditions for being used to prepare the first product and is used to prepare the second production
The optimal conditions of object；To reactor scale removal；By recycle sections scale removal；And filling is used for the modifying agent of reactor.
High pressure ethylene polymerization cellular system includes: computer system, reactor, multiple sensors and multiple transmission devices,
The wherein operation order logic of computer system storage optimization receives operation data from multiple sensors, and according to optimization
Operation order logic and operation data control reactor and transmission device.
Summary of drawings
The operation that Fig. 1 describes the optimization for reactor start-up process of display according to an embodiment of the invention is suitable
The outline flowchart of sequence logic.
Fig. 2 describes the new scale removal of unlatching of determination and conversion ratio real-time compared with average conversion differentiation at any time
The timing of circulation.
Detailed description of the invention
Multiple specific embodiments of the invention, version will now be described, including the preferred embodiment that uses herein and
Definition.Although following details description provides specific preferred embodiment, those skilled in the art recognize these embodiment party
Case is only exemplary, and the present invention can be implemented using other modes.Any reference to " present invention " all referring to
Whole is referred to without necessity by one or more of the present invention that claim limits.Using title purpose only
Be for convenience and its do not limit the scope of the invention.
Just as used in the present invention, " high pressure polymerisation " refer in reactor such as tubular reactor and autoclave
Under high reactor operating pressure, such as higher than under 1000 bars (100MPa) and up to 3000 bars (300MPa) or higher pressure
The polymerization reaction of the high exothermic heat of progress.
Just as used in the present invention, Distributed Control System (DCS) refers to the control system for process or device,
Middle controlling element distribution is in the entire system.DCS typically uses the processor of custom design as controller and uses specially
With both interconnection and standard communication protocol for communication.Output and input the component part that module forms DCS.Processor receives
Information from input module and send information to output module.Input module receives the input in process (or region)
Instruction is passed to the output equipment in region by the information and output module of equipment.It outputs and inputs and can be consecutive variations
Analog signal or discrete signal in two states opened or closed.Computer bus and electronic busses pass through multi-wad join
Device or demultiplexer connection processor and module.Bus also links together the controller of dispersion and master controller and most
It is connected to man-machine interface (HMI) or operation bench eventually.DCS is for controlling the manufacturing process accomplished continuously or intermittently carried out.DCS is connected to biography
Sensor and transmission device and using position control so as to control material run through device flowing.Most common example is by pressure
The setpoint control circuit of sensor, controller and control valve composition.It sends pressure or flow measurements to controller, leads to
Often assisted by Signal Regulation input/output (I/O) device.When the variable of measurement reaches certain point, controller indicate valve or
Transmission device is opened or closed until process fluid flow reaches desired set point.Typical DCS is by a control cabinet
It is able to carry out the function and/or geographical distribution digitial controller composition of 1 to 256 or more management control loops.Input/output
Device (I/O) can with controller integrate or by local area network it is remotely located.The controller of today has extensive calculating energy
Power, and in addition to ratio, logic and sequential control usually may be implemented except integral and derivative (PID) control.DCS is generallyd use
Numerous processors is designed to enhance the reliability of control system.Most systems are with display and configuration software, their energy
Terminal user is enough set to configure control system without carrying out low-level programming, this permission user, which can also preferably pay close attention to, to be answered
With rather than equipment.However, it is necessary to which considerable systematic knowledge and skill are reasonably to configure hardware, software and application program.
Many factories have special staff concentration in these work, this is by may include that the seller of maintenance support contract supports to expand
?.DCS can be used one or more work stations and can configure at work station or be matched by offline personal computer
It sets.By using twisted pair, coaxial or fibre-optic cable control network processes local communication.At server and/or application program
Reason device may include in systems for additional calculating, data collection and reporting capabilities.
Just as used in the present invention, procedural operation (Procedural Operation, ProcOp) refer to by
The application program of Honeywell International exploitation helps user's automation or management operation sequence.It is provided
About the state of execution, the information and feedback intuitive, gradually of switch condition and related process variable keep calling program effectively complete
At release operator is used for other tasks.Using ProcOp, user can be with automation process, this depends on their existing and phases
The automatization level of prestige.In addition, procedural operation can be realizedThe automatic control of interior offline manual process
System.Control system can be interacted with operator for manual process, provide instruction and alarm, be such as used for safety and reliable operation
Writing program in provide as.It is shown using the list and flow chart that pre-establish to use function to fill format to behaviour
Author shows all procedural execution states.In addition, it, which provides operator-central program, executes state and in active tasks
Appear in correct information in face of operator.A part of Experion PKS system provides list for all operations
Solely, consistency environment, no matter it is the behavior of operator, automatic monitoring, automatically controls or alarm.
In the method for the invention, the data of prior operation are collected.This data can be sensed based on the experience of operator
Device is read, equipment specification, method specification, raw material property data, product characteristics data, secure threshold data, and operation refers to
Show with the audio or video of practical operation record etc..
Establish later includes the database for collecting prior operation data.Experienced engineer and operator can be at them
Brain in, on paper or on the physical medium that other tradition use establish database.It is preferred that database purchase is situated between in electronics
In matter such as computer.By modern computer with the ability of higher-order logic and the capture of organized order and storage mass data
To record useful data from substantial all prior operations.Advantageously, by the data in database point
Class indexes and is easily to extract.
Then for analytical database to determine the one or more steps carried out in the operation of current and future, triggering should
The condition of step, using the condition of the step, the duration of step and the order of step.This analysis can partly lead to
Cross human brain progress, such as the judgement of experienced operator or engineer.Selectively, this analysis can be based on predetermined
Algorithm or using artificial intelligence by computer system progress.This analysis can be based on small data group or big data group.?
In latter, the high level computer with deep learning ability can be advantageously used for improvement of mining method opportunity.
The operation order logic of optimization is the one group of possible operating procedure connected by logical relation tree.These operation steps
It suddenly can be by obtaining and collecting based on science and engineering philosophy and from experienced operator before and engineer there
Knowledge is set with device and method handbook or legitimacy demand such as law and rule of the plurality of devices from manufacturer
It counts and is included in sequential logic.The starting of each specific steps, the duration, operating condition, its termination and
Similar factor can be determined by one or more process variables.The order of multiple steps can also be determining by multiple variables,
This can at any time, and be fluctuated from operating to operating.Variable can be over time according to the equipment age, feed material variation, certainly
Right environmental change etc. changes.It is therefore highly desirable to which the operation order logic of optimization is optimised before each operation, to the greatest extent may be used
The course learnt before consideration more than energy.Optimization one or more of can take the following form, and in particular: (i) is in logic
New branch is added or deleted on relational tree；(ii) parameter for causing step starting or terminating is added or deleted；(iii) change true
Determine the threshold value of the parameter during step continues；(iv) change the function for calculating the step duration；And it (v) is directly changed
Process condition, such as temperature, pressure, flow etc..Optimization can be used for it is one or more can different purpose at any time, example
Such as: (a) maximizing output；(b) guarantee product qualities；(c) guarantee safety；(d) energy saves；(e) cost reduces；And class
Like purpose.
Any current operation of system all includes for example supplying from sensor, raw material supplier, equipment supply quotient, public work
Trader collects current operation data to be in the observation of the calculating first operated or logical derivation, operator at the scene etc..It is expected that
, current operation data are automatically generated by sensor and are sent in computer system later for handling.
Then current operation is carried out based on the operation data of collection according to the operation order logic of optimization.Current data can be with
According to the operation order logic of optimization for determining practical operation sequence of steps, the starting and termination of specific steps, each step
Duration, run the condition of the step.It can be desirable to the system is real time monitoring, any input data all can be immediately
It send and calculates correct step and their sequence at once to computer system, and send an instruction to transmission device, other
Equipment, and the correct time and it is as fast as possible control, lagged with minimum time.Including the big of many components
The reliable and balance movement of type complex reaction system under various conditions can be benefit greatly from automation " intelligence of the invention
Can " method.
An advantage of the present invention is that it remembers the positive and passive class about process and equipment learnt before
Journey, to allow course optimization process and the equipment based on study, to consider to have different preferential horizontal many differences simultaneously
Variable is made optimization to process and equipment variations with highest speed and is determined, and by identical system using high-quality and
Reach the flexible manufacture of multi-products short operation cycle.
In a kind of embodiment, the method for operating High pressure ethylene polymerization unit may include that operation reactor opens
Dynamic, the trade mark is converted, reactor scale removal, and recycle sections scale removal and the modifying agent for starting are filled, wherein reactor start-up, board
Number conversion, recycle sections scale removal and for starting modifying agent fill at least one of by optimization operation order logic
To operate.
Reactor start-up
In the preferred embodiment that method wherein of the invention is used to operate reactor start-up, the operation of optimization is suitable
Sequence logic can change with the detailed process of different factories, but typically from secondary compressor is started to making from reactor
Operation sequence is automated in normal condition.
Once operator starts reactor production line, it is automatically collected about the data finally shut down and operator is defeated
What enter during shutdown about data machine operation occurs.In a preferred embodiment, in reactor start-up
The operation order logic of optimization can between initial conditions later differentiation so as to therefore from different starting point startup programs
Path: (a) whether reactor occurs of short duration or extended shutdown；(b) whether occur when preparing vinyl acetate (VA) trade mark
It shuts down；(c) whether need to carry out oxygen analyzer detection；(d) test reactor pressure whether is needed；(e) it is compressed during shutting down
Whether machine cylinder changes；Whether and (e) shutting down is emergency shutdown or controlled shutdown.
In another embodiment, with reference to Fig. 1, the operation order logic optimized in reactor start-up includes extracting operation
The step of middle reactor point, the step are not completed until all reactor points (number that X is reactor point) are put into operation simultaneously.?
In one preferred embodiment, extract operation in reactor point the step of before, the operation order logic of optimization is further
The following steps are included: (a) operator checks and confirms that (Kernel-based methods instruct (PD) and/or follow from last operating log-on data
The data of ring)；(b) check valve position；(c) start the second compressor；(d) operator confirms the second compressor start；(e) it examines
It looks into extruder parameter and sets JWS, preheater, and purified purge gas unit (PGPU) flows；(f) modifying agent stream is opened；
(g) it progressivelyes reach goal response device pressure and washes away all initiator pumps；(h) it sets compressor restrictive condition and reduces and change
Property agent stream；(i) check that quenching production line is idle；(j) it waits JWS to reach target and checks that it is idle for squeezing out machine production line
's；(k) exhaust gas pressure is set, high pressure separates (HPS) level and low pressure separation (LPS) is horizontal.Preferably implement at another
In scheme, extract operation in reactor point the step of after, the operation order logic of optimization further comprise adjustment compressor
Restrictive condition and the step of reduce JWS temperature.Step (a) is in place to the project in (k) after last operation cycle
When, the operation order logic of optimization can directly start using the step of extracting reactor point in operation.
During execution, the operation order logic of the optimization in reactor start-up can keep monitoring exceptional condition and, such as
If fruit detects, adequate measures can be taken to solve for failure at once while stopping normal operating.The reality of exceptional condition
Example includes but is not limited to following scenario described: (a) point loss；(b) oxygen is detected；(c) low-steam pressure；(d) modified agent flux deviates
It is expected that flow；(e) there is back pressure alarm when extraction reactor point in use；(f) activation of interlock.
Also in another embodiment, the operation order logic of the optimization in reactor start-up is suitable using procedural operation
Sequence is operated based on up to a hundred inputs for the automation of start-up operation and is more than 20 controllers.Program runtime can be with
It is about 4 to 5 hours.
The operation order logic of optimization in reactor start-up can carry out 10 simultaneously and act and continuously estimate multinomial
Condition substantially increases operating efficiency obtained by experienced operator.It can be with using this program in reactor start-up
Save the probability that loses during reactor start-up operation, and thus also can solve including production loss, substandard product and
The problem of equipment dependability.
Trade mark conversion
In one embodiment, wherein the operation order logic optimized is used for the operation of trade mark conversion, the behaviour of the optimization
Making first since the last batch of of the old trade mark to new grades of sequential logic terminates to automate operation sequence.
In a preferred embodiment, the operation order logic optimized in trade mark conversion may include changing to cause
Agent, reactor pressure, temperature of reactor, modified agent flux and the control of JWS temperature.
The operation order logic of optimization is not limited to any specific trade mark conversion and it can be used for any of board
Number conversion.Preferably, the trade mark of the present invention conversion is following at least one: from and to the conversion of the VA trade mark, by with to
The conversion of the middle density trade mark is converted initiator code, is converted between propylene, propionic aldehyde (PA) and propane and the mixture of PA
Modifying agent.
During execution, the operation order logic that optimizes can keep monitoring exceptional condition in trade mark conversion, and if
If detecting, suitable behavior can be taken to solve for failure at once while stopping normal operating.The reality of exceptional condition
Example includes but is not limited to following scenario described: (a) point loss；(b) back pressure is alarmed；(c) the stick load limitation item on high pressure compressors
Part；And (d) modified agent flux deviates expectation flow.
In another preferred embodiment, the operation order logic optimized in trade mark conversion is suitable using procedural operation
Sequence is used for the automation of trade mark conversion operation.
The probability lost during trade mark conversion operation can be saved using this program in trade mark conversion, and thus
The problem of can solve including production loss, substandard product and equipment dependability.
Reactor scale removal
The starting point of reactor scale removal is suggested by conversion ratio as shown in Figure 2 differentiation at any time.In scale removal-fouling
Average conversion/production in entire circulation will be carried out calculating and continuously be compared with real-time conversion ratio/production.Particularly,
Recycled once beginning to new scale removal when the average conversion started since the circulation of scale removal before is more than real-time conversion ratio, at this moment because
It is persistently reduced from the aspect for average conversion.
In a preferred embodiment, scale removal may comprise steps of: (i) from the JWS of reactor section start to
The JWS of reactor end increases JWS temperature to scale removal target temperature by the water in heating JWS, preferably at about 180 DEG C
To in the range of about 200 DEG C；(ii) holding is determined by calculating scale removal degree based on the relevance of JWS temperature and firing temperature
All temperature be their own scale removal target temperature for a period of time；And temperature is reduced to formula value by (iii), such as less than
90 DEG C, also from the section start of reactor to end.
Typically, the relevance of JWS temperature and firing temperature is almost linear until scale removal starts, can be typically
The reference reaction device inlet temperature of every entrance area from no side logistics.From the point, linear correlation disappear, this be because
Heat transference efficiency is caused to change for scale removal, that it changes physical environments.Stop increasing if deviateing linear relevance, i.e., it is considerable
It observes there is no physical change, shows no longer to carry out scale removal, reaching this moment stops scale removal then to prevent capacity loss.
During scale removal, generates a small amount of polyethylene and thus need to change modifying agent stream.Therefore, it adjusts and is modified in many places
At agent concentration set point, such as up to 30, on the time point of scale removal process.This change depends on the specific operation trade mark
And it is determined by heuristic data.
The automation of reactor scaling operation can consistently carry out scale removal by means of programming in each reactor
Expert avoid capacity loss and it is unqualified production reach utmostly.
Recycle sections scale removal
In a preferred embodiment, wherein the operation order logic optimized is used for recycle sections scaling operation,
The operation order logic of the optimization makes the temperature of the heat of each unit, centre and low cooler raise and reduce automation, and
And change modifying agent control and reactor peak temperature, while considering that stick loads restrictive condition.
In recycle sections scale removal using this program can save lost during recycle sections scaling operation it is several
Rate, and the problem of thus also can solve including production loss, substandard product and equipment dependability.
Modifying agent filling when starting
In a preferred embodiment, wherein the modifying agent when operation order logic optimized is used to operate starting is filled out
It fills, the operation order logic of the optimization is automatically injected a certain amount of modifying agent after actuation.The amount of modifying agent passes through for specific
The total amount of remaining modifying agent and VA in the concentration and unit of modifying agent needed for the trade mark and determine, wherein the former instruction in operator
With in experience range and the latter then needs following more complicated analysis.It, will be anti-for modifying agent remaining in determination unit and VA
Device production line is answered to split into several sections, i.e. reactor, high pressure recycle, secondary compressor, high-pressure separator etc..For each
The minimum pressure that section record starts since parking refills it by pure ethylene for determining minimum content in the section, at it
Before.For each section, based on the minimum content and the remaining modifying agent of concentration calculation and VA when shutting down.It is remaining in whole system
Modifying agent and VA can be determined by the total amount of remaining modifying agent in all sections, and for modified needed for the specific trade mark
The concentration of agent combines, in that case it can be decided that the appropriate amount for the modifying agent for being used to inject at once after starting is to avoid mechanical problem and not
Good quality.
The present invention also provides the systems for operating High pressure ethylene polymerization unit.For operating High pressure ethylene polymerization unit
System can reactor start-up, trade mark conversion, reactor scale removal, recycle sections scale removal and starting when modifying agent filling in
At least one in include optimization of the present invention operation order logic.
In one embodiment, High pressure ethylene polymerization unit can by during polymerization reaction reactor start-up,
It is of the present invention at least one of modifying agent filling when trade mark conversion, reactor scale removal, recycle sections scale removal and starting
The operation order logic of optimization operated.
All documents of the present invention are all by reference to being fully incorporated the present invention, unless otherwise indicated.When in the present invention
When listing numerical lower limits and numerical upper limits, it is expected the range from any lower limit to any upper limit.Due to foregoing general
Illustrate and particular embodiment will be apparent from, it, at that time can be with although illustrate and describing form of the invention here
Various deformation is carried out to improve without departing from the spirit and scope of the present invention.Therefore, the present invention is not intended to be defined by it.
Claims (25)
1. a kind of method for operating High pressure ethylene polymerization unit, comprising:
(I) data from prior operation are collected；
(II) foundation includes the database for the data collected from prior operation；
(III) database is analyzed；
(IV) the operation order logic of optimization is established；
(V) current data of current operation is collected；And
(VI) current operation is carried out according to the operation order logic and current data of optimization.
2. the method for claim 1 wherein step (IV) includes establishing the computer volume for the operation order logic for embodying the optimization
Code.
3. the method for claim 1 or claim 2, wherein step (VI) is at least partially through using automated computer system
System carries out.
4. the method for any one of preceding claims, the process including starting reactor in vinyl polymerization unit, the process
Including at least step (IV), (V) and (VI).
5. method for claim 4, the operation order logic wherein optimized in step (IV) at least considers following procedure variable:
(a) the reactor device that whether reacts shuts down shutdown that is upper of short duration or extending time span；
(b) whether shut down when preparing vinyl acetate (VA) trade mark of polyethylene；
(c) oxygen analyzer inspection whether is needed；
(d) whether reactor pressure is needed to test；
(e) whether compresser cylinder changes during shutting down；And
(f) whether shut down is that emergency shutdown or control are shut down.
6. claim 4 or method for claim 5, wherein the operation optimized in the step of process of starting reactor (IV) is suitable
Sequence logic includes the steps that extracting reactor point in operation.
7. method for claim 5, wherein the operation order logic optimized further comprises the reactor in executing extraction operation
Decide whether to carry out the sequence of following one or more steps and they before the step of point:
(a) it is checked by operator and confirms log-on data；
(b) check valve position；
(c) the second compressor is opened；
(d) operator confirms that the second compressor is opened；
(e) it checks extruder parameter and sets collet water system (JWS), preheater and purified purge gas unit (PGPU) stream
It is dynamic；
(f) modifying agent stream is opened；
(g) it progressivelyes reach goal response device pressure and washes away all initiator pumps；
(h) it sets compressor restrictive condition and reduces modifying agent stream；
(i) check that quenching production line is idle；
(j) it waits JWS to reach target and checks that it is idle for squeezing out machine production line；And
(k) exhaust gas pressure is set, high pressure separates (HPS) level and low pressure separation (LPS) is horizontal.
8. claim 6 or method for claim 7, wherein the operation order logic optimized further comprises in extracting operation
The step of adjusting compressor restrictive condition after the step of reactor point and reducing JWS temperature.
9. the method for any one of claim 4 to 8, wherein the operation order logic use of the optimization in reactor start-up is used for
The measure of procedural operation order.
10. the method for any one of claim 4 to 9, wherein the operation order optimized when one of the following conditions occurs is patrolled
Collect interrupt operation: (a) point loss；(b) oxygen is detected；(c) low vapor pressure；(d) modified agent flux deviates desired flow；
(e) the back pressure alarm when extraction reactor point in operation；And (f) activation of interlock.
11. the method for any one of claims 1 to 3, wherein this method includes that will operate from optimization to be used to prepare the first product
Condition be converted to optimization be used to prepare the second product condition process, the process include at least step (IV), (V) and
(VI) and the optimization operation order logic the step of conversion in (IV) since the preparation of the first product of last batch of to
The preparation of a collection of second product terminates.
12. the method for claim 11, wherein the operation order logic of the optimization in switch process includes adjustment initiator, reaction
One or more of device pressure, temperature of reactor, modifying agent substance, modified agent flux and the control of JWS temperature.
13. the method for claim 11 or claim 12, wherein at least one of the following is applicable in:
(a) the first product is vinyl-vinyl acetate copolymer, and the second product is Alathon；
(b) the first product is Alathon, and the second product is vinyl-vinyl acetate copolymer；
(c) the first product is high density polyolefins, and the second product is middle density polyolefin；And
(d) the first product is middle density polyolefin, and the second product is high density polyolefins.
14. the method for any one of claim 10 to 13, wherein the operation optimized when one in the following conditions occurs is suitable
Sequence logical break normally operates: (a) point loss；(b) back pressure is alarmed；(c) stick on high pressure compressors loads restrictive condition；
And (d) modified agent flux deviates desired flow.
15. the method for any one of claim 10 to 14, wherein the operation order logic of the optimization in trade mark conversion uses use
In the measure of procedural operation order.
16. the method for any one of claims 1 to 3, wherein the method includes since flat when previous scale removal circulation
Equal conversion ratio starts the process to reactor scale removal when being more than real-time conversion ratio, the process include at least step (IV), (V) and
(VI)。
17. the method for claim 16, wherein the operation order of the optimization in the step of to the process of reactor scale removal (IV) is patrolled
Collecting includes: (a) from the JWS of reactor section start to the JWS of reactor end, increases jacket water (J.W.) system temperature to scale removal target
Temperature；(b) all temperature are remained into their own scale removal target temperature for a period of time；And it (c) is originated from reactor
Locate that temperature is reduced to formula value to end.
18. the method for claim 17, wherein scale removal target temperature is between about 180 DEG C to about 200 DEG C.
19. the method for claim 17 or claim 18, wherein described a period of time passes through based on JWS temperature and igniting temperature
The relevance of degree calculates scale removal degree and determines.
20. the method for claim 19, wherein the relevance is linear correlation until scale removal starts.
21. the method for claim 20, wherein being removed stopping reactor at the time of stopping increasing from the deviation of linear correlation
Dirt.
22. the method for claim 17, wherein the formula value in step (c) is 90 DEG C or less.
23. the method for any one of claims 1 to 3, the method includes at least executing step (IV), (V) and (VI)
The process of recycle sections scale removal, in which:
The process includes the chiller temperature that each unit is raised and lowered automatically, and changes modifying agent control and reactor peak
It is worth temperature.
24. the method for any one of claims 1 to 3, wherein this method include at least execute step (IV), (V) and
(VI) process of reactor filling modifying agent, wherein
The process includes being automatically injected a certain amount of modifying agent after actuation.
25. the method for claim 24, wherein step (IV) includes the concentration according to (a) for modifying agent needed for the specific trade mark；
And (b) in the unit total amount of remaining modifying agent and VA determine the amount of modifying agent.
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| US62/356,846 | 2016-06-30 | ||
| PCT/US2017/028601 WO2018004792A1 (en) | 2016-06-30 | 2017-04-20 | Methods and systems for operating a high pressure ethylene polymerization unit |
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| CN109300514B (en) * | 2018-09-17 | 2020-01-14 | 华南理工大学 | Method for predicting laser glass performance by adopting glass material gene method |
| EP4065674B1 (en) * | 2019-11-27 | 2024-05-01 | Borealis AG | Polybutene-free lubricating composition |
| CN115536763B (en) * | 2022-08-26 | 2023-10-31 | 金澳科技（湖北）化工有限公司 | SPG process sis logic optimization method |
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| Publication number | Publication date |
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| US11636923B2 (en) | 2023-04-25 |
| CN109564771B (en) | 2023-11-21 |
| WO2018004792A1 (en) | 2018-01-04 |
| EP3479261A1 (en) | 2019-05-08 |
| KR20190013983A (en) | 2019-02-11 |
| MY193476A (en) | 2022-10-15 |
| KR102396612B1 (en) | 2022-05-12 |
| US20190244682A1 (en) | 2019-08-08 |
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